CN201241063Y - Circulation discontinuous type ethoxy or propoxy production apparatus - Google Patents
Circulation discontinuous type ethoxy or propoxy production apparatus Download PDFInfo
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- CN201241063Y CN201241063Y CNU2008201163345U CN200820116334U CN201241063Y CN 201241063 Y CN201241063 Y CN 201241063Y CN U2008201163345 U CNU2008201163345 U CN U2008201163345U CN 200820116334 U CN200820116334 U CN 200820116334U CN 201241063 Y CN201241063 Y CN 201241063Y
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Abstract
The utility model relates to a cycle discontinuous ethoxylation or propoxylation preparation device, which comprises a first-level reactor (6), a second-level reactor (7), a third-level reactor (8), a storing tank (1), an impulse reducing device (4), a head exchanger I (5), a cycle pump (9), a head exchanger 2 (10) and mixing nozzles (18); the mixing nozzle (18) is respectively arranged on three levels devices; the storing tank (1) is connected with the head exchanger I (5) which is respectively connected with gas inlets which are arranged on the mixing nozzles (18) of the three-level reactor; a cycle liquid discharging outlet III (8.2)of the third-level reactor (8) is communicated with the second-level reactor (7) which is communicated with the first-level reactor (6); a cycle liquid discharging outlet I (6.2)of the first-level reactor (6) is connected with the cycle pump (9) outlet which is connected with the head exchanger II (10) inlet; and the head exchanger II (10) outlet is respectively connected with cycle liquid inlets (18.1)on the mixing nozzles (18) of the first-level reactor (6), the second-level reactor (7) and the third-level reactor (8). The device can save the reaction time by one fourth to one third, and can produce the highly combined composite quantity.
Description
Technical field
The utility model relates to a kind of oxyethyl group or propoxylation production equipment.Belong to field of chemical technology.
Background technology
The principle of operation of traditional oxyethyl group or propoxylation reactor is earlier oxyethyl group or the pressurization of propenoxylated material to be sprayed into reaction chamber, simultaneously liquid epoxy ethane or propylene oxide are imported reaction zone by pump, the circulation fluid reaction of oxyethane that in reaction zone, gasifies or propylene oxide and ethoxylation.Adopt traditional circular gap formula ethoxylation production equipment, be about to the oxyethane liquid meter and add reactor.Its reaction times is 6～8 hours, long reaction time.
Summary of the invention
The purpose of this utility model is to overcome above-mentioned deficiency, provides a kind of reaction times short circular gap formula oxyethyl group or propoxylation production equipment.
The purpose of this utility model is achieved in that a kind of circular gap formula oxyethyl group or propoxylation production equipment, it is characterized in that described device comprises: A reactor, second reactor, three reactor, basin, strainer, volume pump, subtract pulse jar, interchanger I, recycle pump, interchanger II and mixed jet
Be respectively arranged with a mixed jet on described A reactor, second reactor, the three reactor, circulation fluid opening for feed I, a circulation fluid opening for feed II and circulation fluid opening for feed III, circulation fluid discharge port I, a circulation fluid discharge port II and circulation fluid discharge port III
Described interchanger I is provided with an opening for feed, oxyethane or propylene oxide pneumatic outlet,
Described mixed jet has a circulation fluid import, oxyethane or propylene oxide gas feed, a mixture atomizing outlet,
Described basin outlet links to each other with filter inlet, filter outlet links to each other with the volume pump import, the volume pump outlet links to each other with interchanger I opening for feed, interchanger I air outlet respectively with described A reactor, second reactor and three reactor on mixed jet on oxyethane or propylene oxide gas feed link to each other
Circulation fluid discharge port III is connected with circulation fluid opening for feed II on the second reactor, circulation fluid opening for feed I on circulation fluid discharge port II on the second reactor and the A reactor be connected, circulation fluid discharge port I on the A reactor links to each other with pump inlet, circulating-pump outlet links to each other with interchanger II import, interchanger II outlet respectively with A reactor, second reactor and three reactor on mixed jet on the circulation fluid import link to each other.
Act on improvement of the present utility model, described oxyethane or propylene oxide gasification back spray into A reactor, second reactor and three reactor with circulation fluid after the mixed jet atomizing, therefore atomizing effect is better, react also faster, reactor cycles liquid spraynozzle of tradition is a plurality of, and the utility model is as long as a nozzle, and the alcohol ether of same oxyethane or propylene oxide adduction number (or ester ether, the polyethers) reaction times can save 1/4～1/3.And can produce high adduction number (the epoxide adduction be'ss several more than 40) product.
Description of drawings
Fig. 1 is the overall structure synoptic diagram of the utility model circular gap formula oxyethyl group or propoxylation production equipment.
Fig. 2 is a mixed jet structural representation of the present utility model.
Fig. 3 is a spiral nozzle structural representation of the present utility model.
Fig. 4 is the vertical view of Fig. 3.
Among the figure: basin 1, strainer 2, volume pump 3, subtract pulse jar 4, interchanger I5, A reactor 6, second reactor 7, three reactor 8, recycle pump 9, interchanger II 10, cloth liquid dispense station 11, capture condenser 12, catalyzer 14, other auxiliary agent 15, oxyethane or propylene oxide 16, mixed jet 18.
Embodiment
Referring to Fig. 1, the utility model circular gap formula oxyethyl group or propoxylation production equipment mainly are made up of basin 1, strainer 2, volume pump 3, subtract pulse jar 4, interchanger I 5, A reactor 6, second reactor 7, three reactor 8, recycle pump 9, interchanger II 10, cloth liquid dispense station 11, capture condenser 12 and mixed jet 18.
Described reactor adopts three grades, is equipped with chuck.Each stage reactor all has an opening for feed 6.1,7.1,8.1, a discharge port 6.2,7.2,8.2, a pressure gauge connection 6.4,7.3,8.3, a temperature-measuring port 6.5,7.4,8.4, second reactor 7 and three reactor 8 chucks have a water vapor import 7.5 and 8.5, and a steam condensation water outlet 7.6 and 8.6 is arranged.A reactor 6 has the charging opening 6.6 of a catalyzer 14 and other auxiliary agent 15, a nitrogen inlet 6.7 is arranged, a vacuum system interface 6.8, chuck have a water vapor import 6.9 and one to coagulate water out 6.10, also have a circulating water intake 6.11 and recirculated water backwater outlet 6.12.When cooling, chuck feeds recirculated water.Interchanger I5 has oxyethane or propylene oxide feed mouth 5.1, and oxyethane or propylene oxide pneumatic outlet are arranged, and chuck has a hot water inlet 5.3 and a hot water outlet 5.4.Cloth liquid dispense station 11 has inlet mouth 11.1, air outlet 11.2, relief valve port 11.3, gauge port 11.4, nitrogen inlet 11.5, valve tube interface 11.6 and 11.7.Described mixed jet 18 has a circulation fluid import 18.1, oxyethane or propylene oxide gas feed 18.2, a mixture atomizing outlet 18.3, as Fig. 2,3.
Working process of the present utility model is: at first use nitrogen replacement entire reaction system before production, reach level of safety.At first, feed steam in the chuck with A reactor 6, A reactor 6 is preheated to 110 ℃, stoichiometric alcohol (or alkylphenol or organic acid or other initiator), catalyzer are added A reactor 6, oxyethane or propylene oxide 16 are pressed into and use the qualified basin of nitrogen replacement 1, liquid epoxy ethane or propylene oxide filter through filter 2, by volume pump 3 meterings stoichiometric oxyethane or propylene oxide are transported to interchanger I5, enter the mixed jet 18 on the A reactor 6 after oxyethane or the propylene oxide gasification.
Beginning oxyethyl group or propoxylation are reflected in the A reactor 6 and carry out, and come the circulation fluid of self-circulating pump 9 and interchanger II 10 and oxyethane or propylene oxide gas to enter A reactor 6 through mixed jet.When speed of response descends, or oxyethane or propylene oxide consumption are when having acquired a certain degree, open second reactor 7, three reactor 8 successively, the cooling of interchanger II 10 usefulness hot water, when system pressure surpassed control pressure, available volume pump 3 regulating ring oxidative ethanes or propylene oxide were failed the material amount, to reduce oxyethane or propylene oxide feed amount, after oxyethane or propylene oxide add to manipulated variable, the system pressure drop low controlling-pressure, oxyethyl group or propoxylation reaction are promptly finished.Other control method is identical with traditional circular gap formula oxyethyl group or propoxylation production control method.
Implementation column 1:
Prescription:
Lauryl alcohol 312kg/ still
Oxyethane 2422kg/ still
Potassium hydroxide 1.56kg/ still
Glacial acetic acid 1.7kg/ still.
Operation:
1, reactive system is qualified with the high pure nitrogen displacement.
2, A reactor 6 chucks lead to steam, A reactor 6 heated up and surpass more than the lauryl alcohol fusing point, with vacuum with the stoichiometric lauryl alcohol of fused by opening for feed 6.1 suction A reactors 6.Close inlet valve, catalyzer potassium hydroxide is closed vacuum system by charging opening 6.6 suction A reactors 6.Use the nitrogen replacement secondary, keep the 0.1Mpa nitrogen pressure.
3, A reactor 6 material temperature controls are reached about 110 ℃, open the bottom valve of A reactor 6 bottoms, start recycle pump 9, the mixed jet of circulation fluid on A reactor 6 returned A reactor, after stoichiometric oxyethane is controlled feed rates through filter 2 by volume pump 3 by oxyethane basin 1 simultaneously, liquid epoxy ethane at interchanger I 5 hot water heating and gasifying, is sprayed into A reactor 6 with the atomizing of circulation fluid in the mixed jet.
4, the addition reaction of circulation fluid and oxyethane is thermopositive reaction, and the control reaction pressure is less than 0.6Mpa during reaction, and temperature is less than 165 ℃, and circulation fluid chuck in interchanger II 10 is lowered the temperature with hot water.
5, first order reaction circulation is normal, opens two, three reactor steam, opens communicating valve, opens two, the circulation fluid feed valve and the oxyethane intake valve of three reactor, closes the circulation fluid feed valve and the oxyethane air intake valve of A reactor.Control pressure is less than 0.6Mpa, and temperature is less than 165 ℃, and is fast if pressure rises, and can regulate oxyethane volume pump 3, reduces feed rate, otherwise increases the inlet amount of oxyethane.And regulate the circulation fluid temperature according to the cooling hot water flooding quantity of interchanger II 10.
When 6, the oxyethane inlet amount reaches manipulated variable, close volume pump 3, closing ring oxidative ethane discharging pump door, after question response pressure was reduced to 0.1～0.2Mpa, reaction promptly finished.
In 3.5～4.5 hours reaction times, after testing, the average adduction number of the oxyethane of product is 40, product proportion 1.071, and 41 ± 2 ℃ of fusing points, 98 ± 1 ℃ of active matter contents, vapour pressure (20 ℃) is less than 133pa, appearance white.
Claims (5)
1, a kind of circular gap formula oxyethyl group or propoxylation production equipment, it is characterized in that described device comprises: A reactor (6), second reactor (7), three reactor (8), basin (1), strainer (2), volume pump (3), subtract pulse jar (4), interchanger I (5), recycle pump (9), interchanger II (10) and mixed jet (18)
Be respectively arranged with a mixed jet (18) on described A reactor (6), second reactor (7), the three reactor (8), a circulation fluid opening for feed I (6.1), circulation fluid opening for feed II (7.1) and circulation fluid opening for feed III (8.1), a circulation fluid discharge port I (6.2), circulation fluid discharge port II (7.2) and circulation fluid discharge port III (8.2)
Described interchanger I (5) is provided with an opening for feed (5.1), oxyethane or propylene oxide pneumatic outlet (5.2),
Described mixed jet (18) has a circulation fluid import (18.1), oxyethane or propylene oxide gas feed (18.2), a mixture atomizing outlet (18.3),
Described basin (1) outlet links to each other with strainer (2) import, strainer (2) outlet links to each other with volume pump (3) import, volume pump (3) outlet links to each other with interchanger I (5) opening for feed (5.1), interchanger I (5) air outlet respectively with described A reactor (6), second reactor (7) and three reactor (8) on mixed jet (18) on oxyethane or propylene oxide gas feed (18.2) link to each other
The circulation fluid discharge port III (8.2) of described three reactor (8) is connected with circulation fluid opening for feed II (7.1) on the second reactor (7), circulation fluid opening for feed I (6.1) on circulation fluid discharge port II (7.2) on the second reactor (7) and the A reactor (6) be connected, circulation fluid discharge port I (6.2) on the A reactor (6) links to each other with recycle pump (9) import, recycle pump (9) outlet links to each other with interchanger II (10) import, and interchanger II (10) exports respectively and A reactor (6), circulation fluid import (18.1) on the mixed jet (18) on second reactor (7) and the three reactor (8) links to each other.
2, a kind of circular gap formula oxyethyl group according to claim 1 or propoxylation production equipment, it is characterized in that described A reactor (6) has the charging opening (6.6) of a catalyzer and other auxiliary agent, a nitrogen inlet (6.7) is arranged, a vacuum system interface (6.8).
3, a kind of circular gap formula oxyethyl group according to claim 1 or propoxylation production equipment, it is characterized in that described A reactor (6) chuck has a water vapor import (6.9) and water out (6.10), a circulating water intake (6.11) and recirculated water backwater outlet (6.12) in addition with fixed attention.
4, a kind of circular gap formula oxyethyl group according to claim 1 or propoxylation production equipment, it is characterized in that described second reactor (7) and three reactor (8) chuck have a water vapor import I (7.5) and water vapor import II (8.5), a steam condensation water outlet I (7.6) and steam condensation water outlet II (8.6) are arranged.
5, a kind of circular gap formula oxyethyl group according to claim 1 or propoxylation production equipment is characterized in that described interchanger I (5) chuck has a hot water inlet (5.3) and a hot water outlet (5.4).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2008201163345U CN201241063Y (en) | 2008-05-08 | 2008-05-08 | Circulation discontinuous type ethoxy or propoxy production apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2008201163345U CN201241063Y (en) | 2008-05-08 | 2008-05-08 | Circulation discontinuous type ethoxy or propoxy production apparatus |
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| Publication Number | Publication Date |
|---|---|
| CN201241063Y true CN201241063Y (en) | 2009-05-20 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNU2008201163345U Expired - Fee Related CN201241063Y (en) | 2008-05-08 | 2008-05-08 | Circulation discontinuous type ethoxy or propoxy production apparatus |
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| CN (1) | CN201241063Y (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105001411A (en) * | 2015-05-22 | 2015-10-28 | 江苏苏博特新材料股份有限公司 | Production device and method for special high-molecular-weight polyether macromonomer for polycarboxylate superplasticizer |
| CN114685263A (en) * | 2020-12-31 | 2022-07-01 | 中国石油化工股份有限公司 | Method and device for preparing dimer acid |
-
2008
- 2008-05-08 CN CNU2008201163345U patent/CN201241063Y/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105001411A (en) * | 2015-05-22 | 2015-10-28 | 江苏苏博特新材料股份有限公司 | Production device and method for special high-molecular-weight polyether macromonomer for polycarboxylate superplasticizer |
| CN105001411B (en) * | 2015-05-22 | 2017-03-01 | 江苏苏博特新材料股份有限公司 | A kind of process units of the special high molecular weight polyether polymeric monomer of polycarboxylate water-reducer and method |
| CN114685263A (en) * | 2020-12-31 | 2022-07-01 | 中国石油化工股份有限公司 | Method and device for preparing dimer acid |
| CN114685263B (en) * | 2020-12-31 | 2024-05-07 | 中国石油化工股份有限公司 | Preparation method and device of dimer acid |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20090520 Termination date: 20110508 |